Apparatuses, systems and methods for efficient solubilization of carbon dioxide in water using high energy impact

ABSTRACT

A method for the efficient solubilization of carbon dioxide in water through the use of high energy impacts is disclosed. The method can optionally includes mixing the carbon dioxide and water to form an annular dispersed flow, accelerating the carbon dioxide and water prior to the collision; providing a retention network to collect the carbonated water flow. Also disclosed are systems and apparatuses for practicing the disclosed methods.

FIELD OF THE INVENTION

The present disclosure relates to apparatuses, systems and methods forsolubilizing gases into liquids and, in particular, creating carbonatedbeverages for human consumption.

BACKGROUND OF THE INVENTION

Water and carbon dioxide are generally immiscible under normalenvironmental conditions, i.e., room temperature and atmosphericpressure. Apparatuses and methods are known for producing carbonatedwater by creating conditions under which carbon dioxide will becomewater-soluble. Generally, carbon dioxide becomes more soluble in wateras pressures increase and temperatures decrease.

Most commercialized devices for carbonating water use carbon dioxidesprayed into a water container: the result obtained with this process isvery poor and the carbonation of water is weak and does not last toolong. Devices for producing and dispensing carbonated beverages in waterdispensing units, instead, typically employ a carbonating tank, called asaturator, and a high-pressure water pump. Carbonated water is producedby pressurizing the saturator tank with carbon dioxide and filling thetank with chilled water. Due to the high pressures resident in thesaturator tank, typically around 70 psi, a relatively expensivehigh-pressure water pump is required to inject water into the tank.Furthermore, under the conditions in the saturator tank, the carbondioxide takes time to dissolve into to the water and achieve a palatablelevel of carbonization. Accordingly, the saturator is typically largeenough to hold a ready supply of carbonated water for dispensing anddoes not create new carbonated water instantaneously on demand. Tomaintain this supply, two or more sensors—and associated electroniccontrols—are used to start the high pressure pump and inject water intosaturator when the level of carbonated water in the saturator fallsbelow a set threshold and then stop the water injection when the tankfills to an appropriate level.

These typical carbonization devices take up a relatively large amount ofspace and require expensive and complicated electronic and hydrauliccontrol systems. Due to this complex structure, these devices are noisy,use significant amounts of energy, and require frequent maintenance.

SUMMARY OF THE INVENTION

The embodiments of the disclosed inventions teach efficient andinexpensive methods, apparatuses and systems for the solubilization ofcarbon dioxide in water.

In accordance with one exemplary embodiment of the present disclosure amethod for solubilizing carbon dioxide in water is taught. The methodbegins with the injection of water and carbon dioxide into a chamber.There the carbon dioxide and water are mixed to create anannular-dispersed flow in the chamber. This flow is then accelerated anddirected to collide with a rigid surface, thereby creating a pressuresufficient to solubilize the carbon dioxide into the water. Thecarbonated water is then collected for dispensing.

In accordance with another exemplary embodiment of present disclosure anapparatus is disclosed that can be placed in a water line path to createcarbonated water for dispensing. Advantageously, the apparatus acceptscarbon dioxide and water through an inlet path. From there the flow ofcarbon dioxide and water are passed through one or more dispersionelements arranged within the conduit to create a dispersed flow. Thedispersed flow then passes through a passive accelerator within theconduit, thereby greatly increasing the kinetic energy of the system.The accelerated flow is directed to collide with a rigid impact surfaceimmediately downstream of the passive accelerator. This collisioncreates sufficient pressure to solubilize the carbon dioxide into thewater. A retention network is provided at the output of the apparatus tocollect and regulate the flow of carbonated water.

Further embodiments including advantageous aspects of the disclosedmethods, apparatuses and systems are described in the detaileddisclosure. All the disclosures herein are merely exemplary and can bereadily adapted by persons of skill in the art without diverting fromspirit and scope of the disclosed and claimed inventions.

BRIEF DESCRIPTION OF THE FIGURES

The accompanying drawings illustrate various non-limiting,representative, inventive aspects in accordance with the presentdisclosure:

FIG. 1A illustrates a conceptual diagram of one aspect of the disclosedmethods, systems and apparatuses.

FIG. 1B illustrates aspects of the disclosed methods, systems andapparatuses.

FIGS. 2A and 2B are conceptual diagrams illustrating one aspect of thedisclosed methods, systems and apparatuses.

FIG. 3 illustrates an embodiment of a system for use in accordance withthe disclosed methods and apparatuses.

FIGS. 4 and 4A show views of an embodiment of an apparatus for use withthe disclosed systems and methods.

FIGS. 5A-1 to 5A-6 and 5B-1 to 5B-6 are conceptual diagrams illustratingone aspect of the disclosed methods, systems and apparatuses.

FIG. 6 is an embodiment of an apparatus for use with the disclosedsystems and methods.

FIGS. 7 and 7A show views of an embodiment of an apparatus for use withthe disclosed systems and methods.

FIGS. 8 and 8A show views of an embodiment of an apparatus for use withthe disclosed systems and methods.

FIGS. 9 and 9A show views of an embodiment of an apparatus for use withthe disclosed systems and methods.

DETAILED DESCRIPTION OF THE INVENTION

Apparatuses, systems and methods are disclosed herein for the quick andefficient solubilization of carbon dioxide in water. In particular,carbonated water is created through the instantaneous transformation ofkinetic energy into a localized pressure wave to create a region with anenergy density sufficient to solubilize carbon dioxide into water. Thiscan be achieved through the use of an apparatus that sits in-line withthe water supply to create a continuous flow of carbonated water.

One particularly advantageous aspect of the disclosed method is thesolubilization of carbon dioxide in water through the collision of acarbon dioxide/water stream with a rigid surface. FIG. 1A showsconceptual diagram of the interactions occurring in an exemplarycollision in accordance with the present invention.

As shown in FIG. 1A, a carbon dioxide/water stream 2 is directed at arigid surface, such as wall 1. Upon collision with the wall the momentumof the stream 2 is suddenly brought to zero creating a zone of highenergy density and very large local pressure 3. The large pressurecreated by the collision results in the solubilization of the carbondioxide into the water.

In pressure zone 3, huge numbers of instantaneous collisions creatingsolubilization occur between: the carbon dioxide/water mixture and therigid surface; the incoming stream and the carbon dioxide and waterdroplets that have bounced off the rigid surface (i.e., the scatteredmixture); and, the scattered mixture and side walls of the conduitcarrying the stream.

The change in momentum that occurs when the carbon dioxide/water streamcollides with the rigid surface results in a force exerted on thestream. Like all momentum changes, the force applied to create thechange is a function of the period of time over which it occurs. Becausethe momentum changes nearly instantly when the carbon dioxide/waterstream collides with the rigid wall, the force is exercised in a veryshort period of time and is, as a result, extremely large.

The optimal forces generated in the pressure zone, or the pressureenergy densities, that must be obtained in that region for an efficientsolubilization are in the range of between −40 to 5 foot-pound/cm³. FIG.1B is a graph that shows the change in the pressure energy density withrespect to the velocity of the carbon dioxide/water stream. As thevelocity of the carbon dioxide/water stream increases, the pressureenergy density decreases to compensate for the increase in the kineticenergy density. This decrease in pressure energy density is thenconverted to increase the collision forces at the gas/liquid interfaceat the rigid wall 1 and the pressure zone 3.

As the mixed carbon dioxide/water stream collides with the rigid wall,the collision forces generated are instantaneous (at time=0). As timecontinuously advances (time=t₁ . . . t_(n)), further collision forcesare generated between the incoming carbon dioxide and water moleculesand the already solubilized carbon dioxide and water molecules havingdifferent directional velocities. The cumulative chain effect is suchthat the forces act upon each segment of the stream for a given amountof time to further merge the two phases into each other as a result ofcontinuous and instantaneous momentum transfer; thus, producingcarbonated water in which carbon dioxide has been thoroughly andcompletely solubilized.

Structuring the water/carbon dioxide stream can further enhance thesolubilization of carbon dioxide at the collision site. Withoutstructuring the water/carbon dioxide stream will tend to take on astratified arrangement with the carbon dioxide and water flowing insubstantially discrete layers of water 4 and carbon dioxide 7, as shownin FIG. 2A. These layers inhibit optimal solubilization because theyprovide a limited amount of surface area contact between the carbondioxide and the water. This limited surface area of contact reduces theopportunities for the carbon dioxide to solubilize in the water.Structuring the water/carbon dioxide stream to prevent a substantiallylaminar flow corrects this problem.

The general goal of the structuring is to create a dispersed flow ofwater droplets homogenously mixed with the carbon dioxide stream inorder to increase the total surface area of contact between the twosubstances. In practice, the flow pattern never becomes fully dispersedand an annular-dispersed pattern of water 4 and dispersed water andcarbon dioxide 8, as shown conceptually in FIG. 2B, is created. Asshown, the resulting flow will typically have a carbon dioxide corecontaining dispersed water droplets that is surrounded by a relativelythin layer of water along the wall of the channel

Any known mechanism in the art for creating annular dispersed flowscould be adapted to the disclosed methods. For example, this type offlow can be created through stationary mixing elements in the flow path,such as fins protruding from the conduit wall or helical structuresaxially aligned in the flow path.

The solubilization of carbon dioxide into water can be further enhancedby accelerating the carbon dioxide/water stream prior to its collisionwith the rigid wall. Preferably, the acceleration is achieved by forcingthe stream through an accelerator. As is well known in the art, passinga fluid flow through a restriction will result in an accelerated flowarising due to the principle of mass conservation. This can beaccomplished structurally via a simple orifice or more complexengineered structures, such as a Venturi tube.

The accelerator is used to easily increase the kinetic energy of thecarbon dioxide/water stream prior to the collision. Thus, for a giveninlet speed and pressure, the energy of the carbon dioxide/water flowwill be increased without requiring an expensive pumping apparatus. Thisincreased kinetic energy increases the pressure achieved in the pressurezone, which results in improved solubilization at the collision sitebecause more kinetic energy is dissipated.

Acceleration with a restrictor is particularly advantageous when adispersed flow is accelerated. Passing a dispersed flow through arestriction helps ensure that the carbon dioxide and the water areuniformly accelerated, thereby enhancing solubilization upon collisionwith the rigid surface.

After collision with the rigid surface the level of carbon dioxidesolubilization can be further increased by employing a retention networkbetween the rigid wall and the dispenser outlet to regulate the flowprior to dispensing. The retention network allows the carbonated waterto settle to an acceptable pressure for dispensing, for example 10 psito 40 psi. The retention network allows the high-pressure chaotic flowpassing the rigid surface to collect into a regular continuous flow fordispensing.

In addition to creating a suitable flow for dispensing, the retentionnetwork also improves the carbonization process. Filling the retentionnetwork with fluid assists in maintaining pressure at the outlet of thecollision area. This in turn results in a higher pressure inside thepressures zone. In contrast, a relatively low pressure at the outlet ofthe collision area, such as atmospheric pressure, would allow a readyrelease of the pressure built in the pressure zone through the outlet ofthe collision area.

The retention network allows for a relatively high pressure to bemaintained at the collision area outlet, which can be gradually reducedto a proper pressure for dispensing the beverage, for example, 10 psi.

The pressure drop through the retention network depends upon length,width and structure of the network. For example, assuming a constantdiameter, increasing the length of the retention network will increasesthe pressure drop through the retention network. Keeping the diameter ofthe retention network constant at 3/16 inch (0.1875 inch) a retentionnetwork about 10 inches long will create a pressure drop of around 120psi, assuming a starting pressure of about 160 psi.

While the described method of high-energy wall impact described above isalone sufficient to produce carbonated beverages, the combined use of(i) flow structuring dispersion, (ii) accelerators, and, (iii) aretention network after the collisions each operate to a synergisticeffect when installed together in series. In other words, adding eachstep further improves performance of the method and the output product.Using a combination of one or more of these additional steps, preferablyall of them, produced a well solubilized carbon dioxide in watermixture.

The disclosed method for producing carbonated water can further beenhanced through the introduction of a chiller, e.g., a refrigerator orthe like, to reduce the temperature of the water. The chiller wouldpreferably work to cool the water before it enters the system of flowdevelopers, collision walls, and the retention network, but it couldoperate such that chilling occurs in any and all of those locations.

The disclosed method could also be further enhanced by increasing theflow pressure of the water in the system, for example by employing apump in the flow path or a gravity feed from an elevated water supply. Apump or other pressure enhancer, would preferably be positioned prior tothe water being mixed with the carbon dioxide by the flow developers. Apump is particularly useful in commercial embodiments intended to beinstalled in any location because water pressure, especially frommunicipal water lines, can vary from one location to another. To correctthis, a pump can supply a constant pressure into the system. While apump can optionally be used, the method disclosed herein can beaccomplished without a pump.

An exemplary system for practicing the disclosed method is shownconceptually in FIG. 3. The carbon dioxide supply 10 and water supply 20are simultaneously provided to in-line solubilizer 50. The in-linesolubilizer 50 is followed by retention network 60, which is in turnfollowed by dispenser 70.

Carbon dioxide supply 10 can be embodied by any known way for supplyinga gas. A commercially available CO2 canister is preferably used. Thecarbon dioxide supply would typically be connected through a regulator15, which provides a controlled supply pressure to the in-linesolubilizer 50.

The system is further fed by water supply 20. This supply can consist ofa simple municipal or well water feed. Preferably, the water supply 20comprises a chiller to cool the water because carbon dioxide solubilizesmore readily into colder water.

The water supply system 20 also optionally comprises a pump to provide aconsistent water pressure. As discussed above, the pressure at a typicalhome or commercial water tap may vary from location to location or fromtime to time. A pump will ensure that the apparatus receives aconsistent pressure no matter what the local supply pressure is. Thissame goal of providing a consistent supply pressure can be achieved byother known techniques without departing from the scope of thedisclosure. For example, an elevated water reservoir could use gravityand appropriately sized water conduits to provide a consistent watersupply pressure.

An exemplary embodiment of the collision chamber is shown in FIG. 4. Thecarbon dioxide and water are brought into contact via a Y-shaped inletmanifold 400 having two inlets, one for a carbon dioxide supply theother for a water supply. In this embodiment, the two inlets areidentical and interchangeable. The manifold used to introduce the carbondioxide and water into the collision chamber can be of any othersuitable arrangement, for example, T-shaped or F-shaped. As a furtherexample, the supplies could be provided by a concentric tube within atube structure. The Y-shaped manifold, or other shapes depending ontheir need, could also include an initial divider to prevent one streamgoing into the other supplies' inlet. Furthermore, standard backflowpreventers can also be used within the inlets or upstream of the inlets.Furthermore, the flow of water and carbon dioxide can also be controlledby valves or regulators at the entrance of the manifold.

The incoming water pressure affects the flow and pressure through theremainder of the system. A minimum pressure of 10 psi is sufficient toachieve a satisfactory flow rate and carbonation. A flow rate in therange of 0.1 gpm to 1.5 gpm has been found to be particularlyadvantageous, but even higher flow rates are also acceptable.

The carbon dioxide is provided at a pressure between 45 psi and 125 psi.Preferably, the carbon dioxide pressure provided at the Y-shaped inletmanifold is kept close to the water pressure provided at the Y-inletmanifold.

In the embodiment of FIGS. 4 and 4A, flow developers 420 are providedwithin the flow path after the inlet manifold. The flow developers areused in order to prevent a stratified, or laminar, carbon dioxide/waterflow. Instead, the flow developers create a substantially dispersedflow, typically an annular-dispersed flow. The embodiment of FIG. 4 usespassive flow developers comprised of helically shaped elements 520,shown in detail in multiple views in FIG. 5A Other passive directionalmixers capable of dispersing the carbon dioxide and water flow wouldalso be suitable, such as protrusions from the conduit wall.Alternatively, active mixers, such as spinning blades can be used. Asshown in FIG. 4, the flow developing elements 420 can be arranged inseries to achieve the desired level of dispersion. The flow developingelements can similarly be used in combinations of different types,including mixed passive and active elements.

The dispersed stream of carbon dioxide/water is then accelerated byforcing it through a restrictor/accelerator 430. As is well known in theart, passing a fluid flow through a restriction will result in anaccelerated flow, which arises due to the principle of massconservation. The restrictor/accelerator is used to easily increase thekinetic energy of the carbon dioxide/water stream prior to thecollision. Thus, for a given inlet speed and pressure, the energy of theof the carbon dioxide/water flow exiting the restrictor/accelerator willbe increased without requiring an expensive pumping apparatus.

This increased kinetic energy results in a higher momentum change uponimpact with the collision surface 450, thereby increasing the pressureachieved in the pressure zone, which results in improved solubilizationat the collision site. The restrictor/accelerator 430 is a simpleorifice. However, more complex engineered structures, such as a Venturitube, can also be employed.

For a structure having a conduit cross sectional area A1 and arestriction cross sectional area A2, the total momentum, energy and massare conserved and the conserved equations for the carbon dioxide/waterstream can be written as:

Mass:

${\frac{}{t}m_{tot}} = {{{\rho_{1}( v_{1} )}A_{1}} - {{\rho_{2}( v_{2} )}A_{2}}}$

Momentum:

${\frac{}{t}P_{tot}} = {{{\rho_{1}( v_{1}^{2} )}A_{1}} - {{\rho_{2}( v_{2}^{2} )}A_{2}} + \{ {{\rho_{1}A_{1}} - {\rho_{2}A_{2}}} \} - \{ F \} + \{ {m_{tot}g} \}}$

Energy:

${\frac{}{t}( {K_{tot} + Z_{tot} + H_{tot}} )} = {{- {\Delta\lbrack {( {{\frac{1}{2}\frac{( v^{2} )}{(v)}} + Z + G} ){\rho (v)}A} \rbrack}} - W - E_{v}}$

It has been observed that good carbonation levels are achieved when thesmall restrictor/accelerator is designed such that the velocity of theincoming carbon dioxide/water steam is accelerated from one to up to 100times its original velocity through the small passage.

The average velocity for a circular geometry, as for this apparatus, canbe derived as:

$( v^{i} ) = \frac{\int_{0}^{2\; \pi}{\int_{0}^{R}{v^{i}r{r}{\theta}}}}{\int_{0}^{2\; \pi}{\int_{0}^{R}{r{r}{\theta}}}}$

In the above equations:

m_(tot)=total mass of carbon dioxide/water mixture

P_(tot)=total momentum of carbon dioxide/water mixture

K_(tot)=total kinetic energy of carbon dioxide/water mixture

Z_(tot)=total potential energy of carbon dioxide/water mixture

H_(tot)=total Helmholtz (free energy) of carbon dioxide/water mixture

ρ=density

A=cross section

R=radius

−F=a vector representing the net force of the solid surfaces on themixture and collision forces

p=pressure

G=Gibbs free energy

W=rate at which system performs mechanical work

E_(v)=energy loss

When the carbon dioxide/water stream flows through the restriction, suchas an orifice, there is a certain amount of energy loss (Ev). Assuming aquasi-steady flow, the energy loss can be derived as:

E _(v)=½(v)² e _(v)

In the above equation, e_(v), is the loss coefficient which is afunction of the Reynold's number and relates to the efficiency of theinlet to smoothly transition flow from the upstream to the restrictedflow area. Many tabulated data are available to those of skill in theart for estimating the loss coefficient for different geometricalconsiderations. For a sudden contraction or converging restriction, theloss coefficient may be calculated as:

e _(v)=0.45(1−β)

And for a sharp-edged orifice:

$e_{v} = {2.7( {1 - \beta} )( {1 - \beta^{2}} )\frac{1}{\beta^{2}}}$

where β=is the ratio of the restricted area to the area before therestriction

It has been observed that acceptable solubilization in accordance withthis disclosure is achieved with a sudden contraction or a convergingrestriction when it is designed to have a loss coefficient between 0.1to 0.44, preferably about 0.41. For a sharp-edged orifice such asrestrictor/accelerator 430 in FIG. 4, acceptable solubilization occurswith a loss coefficient larger than 10, preferably 60.

In addition, the size of the restrictions can be varied to achieve highquality carbonated water. The ratio of the inlet radius to thecontracted area radius is optimally designed to be in the range between1 (no restriction) and 20 (max restriction);

In the very neighborhood of the moving streamlines of carbon dioxidesurrounded by water passing the restrictions, each stream acquires acertain amount of momentum and related kinetic energy. Thesestreamlines, in turn, impart some of its momentum to the adjacent layerof solution causing it to remain in motion and accelerate further in theflow direction. The momentum flux, in this case, is in the direction ofthe negative velocity gradient. In other words, the momentum tends to goin the direction of decreasing velocity; thus the velocity gradient canbe considered as the driving force for momentum transport.

When the carbon dioxide/water mixture is flowing through the narrowpassage (example: the orifice) parallel to the surfaces, the velocity ofthe mixture in the flow direction decreases as approached to thesurfaces. This velocity difference between the adjacent layers of thecarbon dioxide and water results in a velocity gradient. By randomdiffusion of molecules occurring between faster moving layers ofmolecules and the slower adjacent layer, the momentum is transferred inthe transverse direction within the narrow passage from the faster tothe slower moving layer.

After leaving the restrictor/accelerator 430 the accelerated stream ofcarbon dioxide/water mixture, having reached a much higher kineticenergy, collides with stationary solid wall 450. The solid wall 450 canbe of any shape or structure, preferably the wall is placedperpendicular to the carbon dioxide/water stream. The wall should beplaced sufficiently close to the restrictor accelerator so that theincreased kinetic energy achieved is not substantially lost due tofrictional forces prior to reaching the wall 450. It has been found thatacceptable results are achieved if the solid wall 450 is placed fromapproximately 0.1 inches and 2.0 inches from the restrictor/accelerator,preferably 0.5 inches.

Net forces generated through the collisions with the wall, i.e., thepressure energy densities (“PED”) in the pressure zone, between a rangeof −40 foot-pound/cm³ to 5 foot-pound/cm³ have been found to produceacceptable solubilization. These forces can be created through adjustingthe relative relationships of the geometries of therestrictor/accelerator, the conduit, the level of mixture achieved, andthe starting pressure of the inlet carbon dioxide and water streams.

In an embodiment such as the one shown in FIG. 4, a flow rate of 0.5gpm, inlet radius of 0.365 inch, orifice area of 0.04 inch (contractionratio of 8.63), in which the inlet velocity of 5.15 in/s is accelerated74 times to 382.97 in/s, the corresponding PED values as a function ofinlet water/CO2 pressure is shown in the table below:

Pressure PED (psi) foot-lb/cm³ 20 0.10 40 0.20 60 0.31 80 0.41 100 0.51120 0.61 140 0.71 160 0.81 180 0.92 200 1.02 220 1.12 240 1.22Furthermore, the PED can be varied with respect to the flow rate of thecarbon dioxide/water stream; by keeping an optimum inlet pressure,constant at 100 psi, and doubling the contraction ratio in the aboveexample as shown in the Table below. As can be seen in the Table, thePED is a strong function of the flow rate.

Flow Rate PED (gpm) foot-lb/cm³ 0.1 0.5 0.5 −0.2 0.9 −1.9 1.3 −4.5 1.7−8.1 2.1 −12.6 2.5 −18.1 2.9 −24.5 3.3 −31.9 3.7 −40.3

The wall 450 further has outlet passages 455 to allow the further flowthrough the system. As shown in FIG. 4 this further connects to theinlet of retention network 460. The retention network can simply be aplain conduit. Retention network 460 of FIG. 4 is comprised of statichelical mixers 465. Other types of packing materials, such as raschigrings, could also be used. Further, any of the static or active mixingelements described as suitable for creating a dispersed flow could beput to use in the retention network to further enhance contact andsolubilization of CO2 in water.

The length and configuration of the retention network and the size ofthe packing materials within the retention network can be modified toobtain different levels of carbonation to dispense carbonated water withdifferent levels of solubilization. Generally, longer retentionnetworks, preferably up to 10 inches, raise the carbonization level byallowing more time for mixing contact between the carbon dioxide andwater in the fluid stream. Longer retention networks also increase thepressure at the outlet passages of the collision chamber 455, whichincreases the pressure within the collision chamber and stabilizes theentire flow rate.

The length and composition of the retention network can also be used toobtain a desired pressure at the outlet of the retention network, whichis preferably connected to the beverage dispensing tap. For a retentionnetwork comprising helical static mixers, the pressure drop can becalculated as:

${\Delta \; \rho} = {( {{k_{OL}^{\prime}A} + k_{OL}} )\frac{64}{Re}\frac{L}{D}\frac{1}{2}\rho {\langle v\rangle}^{2}}$

Where:

k′_(OL) and k_(OL) are Reynold's number (Re) dependent constants whichgenerally range between 0.02-0.1 and 3-12, respectively, with theparticular values being readily available in pre-tabulated charts versusReynold's number

L=length of the helical mixers

D=diameter

Re=Reynold's number

As can be seen from the above equation, the pressure drop achievedthrough the retention network is directly proportional to the ratiobetween the length and the diameter (“L/D”). Therefore, one can achievesimilar pressure drops, flow and mixing characteristics by changingeither the length or the diameter or both of the retention network.Packing materials also affect the pressure drop obtained. Generally,smaller size packing materials and longer retention networks increasethe pressure drop.

FIGS. 6 and 6A show an alternate embodiment with inlet manifold 600having two inlets, one for a carbon dioxide supply the other for a watersupply, an inlet chamber preferably having a size of 345 (the valuesprovided give the relative sizes of the various components, thus nounits are provided). Two stages of directional mixers 620 act as flowdevelopers to create an annular-dispersed flow, alternate views of theflow developers 525 are shown in FIGS. 5A-1 to 5A6 and FIGS. 5B-1 to5B-6. Restrictor/accelerator 630 is a simple orifice having a size of 4.The exit of the of the restrictor/accelerator leads to collision chamber635, which has a length of 250. The back wall of the collision chamberis collision surface 650, having outlets 655. The outlets 655 lead tostart of retention network 660, which contains helical static mixers665.

FIGS. 7 and 7A show another embodiment with inlet manifold 700 havingtwo inlets, one for a carbon dioxide supply the other for a watersupply. Flow development and acceleration is accomplished via two stagesof hourglass shaped restrictor/accelerators 735 and 736. As shown,restrictor/accelerator 735 uses two of the hourglass shaped nozzles.Additional nozzles like this can be employed in other embodiments, andeven more nozzles could be used if space permits. The streams exitingthe nozzles of 735 are directed at the rigid surface adjacent to theentry of nozzle 736. Accordingly, this structure creates a first levelof collision based solubilization. Further upon acceleration throughnozzle 736, the stream is impacted on collision surface 750, havingoutlets 755. The staging multiple accelerations and collisions, as isdone in this embodiment could also be applied to other embodiments.Collision surface 750 has outlets 755.

FIGS. 8 and 8A show an alternate embodiment with inlet manifold 800having two inlets, one for a carbon dioxide supply the other for a watersupply. Flow development and acceleration is accomplished via two stagesof flow developing restrictor/accelerators 835 and 836. As shown, thefront wall of flow developing restrictor/accelerator 835 has sidepassages that each lead to an hourglass shaped accelerator nozzle. Theoutlet streams from these nozzles impact the front wall of flowdeveloping restrictor/accelerator 836, which is the same shape andsimilarly has two walls. The flow exiting these nozzles is directed atthe rigid surface adjacent to the entry of nozzle 837, which acceleratesthe flow again for impact on collision surface 850, having outlets 855.

FIG. 9 shows an alternate embodiment with inlet manifold 900 having twoinlets, one for a carbon dioxide supply the other for a water supply.Two stages of helical static mixers 920 act as flow developers.Restrictor/accelerator 930 is a simple orifice. The exit of therestrictor/accelerator leads to collision chamber 935, in which thestream is collided with a knife-like blade 950. The knife-like blade 950creates collisions of streams that spin off the blade creating vorticesand cavitations, which create high pressure zones amenable tosolubilization. The blade can be stable or, preferably, it can beflexibly designed to resonate with the collisions thereby creatingintense points of pressure at the focus of the resonation.

The entirety of this disclosure (including the Cover Page, Title,Headings, Field, Background, Summary, Brief Description of the Drawings,Detailed Description, Claims, Abstract, Figures, and otherwise) shows byway of illustration various embodiments in which the claimed inventionsmay be practiced. The advantages and features of the disclosure are of arepresentative sample of embodiments only, and are not exhaustive and/orexclusive. They are presented only to assist in understanding and teachthe claimed principles. It should be understood that they are notrepresentative of all claimed inventions. As such, certain aspects ofthe disclosure have not been discussed herein. That alternateembodiments may not have been presented for a specific portion of theinvention or that further undescribed alternate embodiments may beavailable for a portion is not to be considered a disclaimer of thosealternate embodiments.

It will be appreciated that many of those undescribed embodimentsincorporate the same principles of the invention and others areequivalent. Thus, it is to be understood that other embodiments may beutilized and functional, logical, organizational, structuralmodifications may be made without departing from the scope and/or spiritof the disclosure. As such, all examples and/or embodiments are deemedto be non-limiting throughout this disclosure. Also, no inference shouldbe drawn regarding those embodiments discussed herein relative to thosenot discussed herein other than it is as such for purposes of reducingspace and repetition.

In addition, the disclosure includes other inventions not presentlyclaimed. Applicant reserves all rights in those presently unclaimedinventions including the right to claim such inventions, file additionalapplications, continuations, continuations in part, divisions, and/orthe like thereof. As such, it should be understood that advantages,embodiments, examples, functional features and/or other aspects of thedisclosure are not to be considered limitations on the disclosure asdefined by the claims or limitations on equivalents to the claims.

1-26. (canceled)
 27. An apparatus for the solubilization of carbondioxide in water comprising: a conduit defining a flow path; an inletmanifold on the proximal end of the conduit, the inlet manifold having afirst branch to receive water and a second branch for receiving carbondioxide; one or more dispersion elements arranged within the conduit; apassive accelerator within the conduit; a rigid impact surface,positioned between 0.1 to 2.0 inches downstream of the passiveaccelerator; and a retention network coupled to the distal end of theconduit.
 28. The apparatus of claim 27, wherein the inlet manifoldcomprises a Y-shaped connector with a carbon dioxide supply on onebranch of the Y-shaped inlet and a water supply on the other branch ofthe Y-shaped inlet.
 29. The apparatus of claim 27, wherein thedispersion elements comprise at least one of static helical mixers andstatic directional mixers.
 30. The apparatus of claim 27, wherein thepassive accelerator comprises a cylindrical orifice.
 31. The apparatusof claim 27, wherein the passive accelerator comprises an hourglassshaped nozzle.
 32. The apparatus of claim 27, wherein the conduit,passive accelerator, and rigid impact surface are configured withrespect to one another such that impact of a flow passing through theconduit at between 0.1 to 3.7 gallons per minute results in pressureenergy densities at the rigid impact surface of between −40foot-pound/cm³ to 5 foot-pound/cm³.
 33. The apparatus of claim 27,wherein a ratio of the cross sectional area of a portion of the conduitimmediately preceding the passive accelerator compared to the crosssectional area of a restriction within the passive accelerator is suchthat the restriction will accelerate the speed of a fluid flow withinthe conduit up to 100 times.
 34. The apparatus of claim 27, wherein therigid impact surface is oriented normal to the flow path through theconduit at an outlet of the passive accelerator and an output opening ofthe passive accelerator is configured such that a straight lineprojection from each point in the output opening along a longitudinalaxis of the conduit intersects the rigid impact surface.
 35. Theapparatus of claim 27, wherein the passive accelerator comprises acontraction or converging restriction having an energy loss coefficientin the range of 0.1 to 0.44.
 36. The apparatus of claim 27, wherein thedispersion element, the conduit, and the passive accelerator are alignedalong a central longitudinal axis.
 37. The apparatus of claim 36,wherein the rigid impact surface defines at least one peripheral flowpath offset from the central longitudinal axis in direction transverseto the central longitudinal axis.
 38. The apparatus of claim 36, whereinthe retention network includes a second helical dispersion elementaligned with the longitudinal axis.
 39. An apparatus for thesolubilization of carbon dioxide in water comprising: a tubular conduitdisposed about a longitudinal axis, extending from an input end to anoutput end, and defining a fluid flow path from the input end to theoutput end; an inlet manifold comprising a first inlet for water, asecond inlet for carbon dioxide, and an outlet in fluid communicationwith the input end of the conduit; a passive accelerator located withinthe conduit, the passive accelerator comprising a restriction of theconduit having a reduced cross sectional area relative to portions ofthe conduit immediately upstream and downstream of the restrictionportion; and a rigid impact surface positioned between 0.1 to 2.0 inchesdownstream of the passive accelerator and filling a central portion ofthe conduit and defining one or more peripheral flow paths locatedoutside of the central portion of the tubular conduit; wherein: thetubular conduit and restriction portion are aligned along a centrallongitudinal axis, and the peripheral flow paths are offset from thecentral longitudinal axis in a direction transverse to the centrallongitudinal axis, and the passive accelerator has an output openinghaving a radial size that is less than the radial extent of the centralportion of the conduit filled by the rigid impact surface.
 40. Theapparatus of claim 39, wherein the conduit, passive accelerator, andrigid impact surface are configured with respect to one another suchthat impact of a flow passing through the conduit at between 0.1 to 3.7gallons per minute results in pressure energy densities at the rigidimpact surface of between −40 foot-pound/cm³ to 5 foot-pound/cm³. 41.The apparatus of claim 40, where the inlet manifold comprises a Y-shapedconnector with a carbon dioxide supply on one branch of the Y-shapedinlet and a water supply on the other branch of the Y-shaped inlet. 42.The apparatus of claim 39, comprising: one or more dispersion elementsarranged within the conduit, wherein the one or more dispersion elementscomprise at least one of static helical mixers and static directionalmixers.
 43. The apparatus of claim 39, wherein the passive acceleratorcomprises a cylindrical orifice.
 44. The apparatus of claim 39, whereinthe passive accelerator comprises an hourglass shaped nozzle.
 45. Theapparatus of claim 39, comprising: a retention network coupled to theoutput end of the conduit, wherein the retention network comprisesstatic mixers.
 46. The apparatus of claim 39, wherein a ratio of thecross sectional area of a portion of the conduit immediately precedingthe passive accelerator compared to the cross sectional area of arestriction within the passive accelerator is such that it willaccelerate the speed of a fluid flow within the conduit up to 100 times.47. The apparatus of claim 39, wherein the rigid impact surface isoriented normal to the flow path through the conduit at an outlet of thepassive accelerator and an output opening of the passive accelerator isconfigured such that a straight line projection from each point in theoutput opening along a longitudinal axis of the conduit intersects therigid impact surface.
 48. The apparatus of the claim 39, wherein thepassive accelerator comprises a contraction or converging restrictionhaving an energy loss coefficient in the range of 0.1 to 0.44.